energies

Article

Study of a Coil Heat Exchanger with an IceStorage System

Yan Li *, Zhe Yan, Chao Yang, Bin Guo, Han Yuan, Jian Zhao and Ning Mei

College of Engineering, Ocean University of China, Qingdao 266100, China; nydzyz@163.com (Z.Y.);yangc@cqu.edu.cn (C.Y.); lzjdmh@126.com (B.G.); hanyuan@ouc.edu.cn (H.Y.); zhaojian@ouc.edu.cn (J.Z.);nmei@ouc.edu.cn (N.M.)* Correspondence: yanli@ouc.edu.cn; Tel.: +86-0532-6678-2073

Received: 31 October 2017; Accepted: 28 November 2017; Published: 1 December 2017

Abstract: In this study, a coil heat exchanger with an ice storage system is analyzed by theoreticalanalysis, numerical analysis, and experimental analysis. The dynamic characteristics of ice thicknessvariation is studied by means of unstable heat conduction theory in cylindrical coordinates, and thechange rule of the ice layer thickness is obtained. The computational fluid dynamics method isemployed to simulate the flow field and ice melting process of the coil heat exchanger. The effectof the agitator height on the flow characteristics and heat transfer characteristics is investigated.The numerical results show that the turbulence intensity of the fluid near the wall of the heatexchanger is the largest with an agitator height of 80 mm. Furthermore, the process of ice meltingis analyzed. The ice on the outer side of the evaporator tube close to the container wall melts fasterthan the inner side and this agrees well with the experimental result. The experimental study onthe process of the operational period and deicing of the coil heat exchanger is conducted and thetemperature variation curves are obtained by the arrangement of thermocouples. It is found that thetemperature of the evaporating tube increases with increasing height in the process of ice storage.

Keywords: coil heat exchanger; ice storage; phase change; unstable heat conduction theory;computational fluid dynamics (CFD) method

1. Introduction

Coil heat exchangers have many advantages and superior performance, and they exist widely inmany engineering fields for enhanced heat transfer. The study of coil heat exchangers is significant tothe optimization of engineering problems.

In the last decade, several studies about coil heat exchangers by means of experimental study andnumerical simulation have been carried out. Marija et al. [1] analyzed the performance of a helical coilheat exchanger by experiment, and the different operating conditions were discussed. Furthermore,the verification of the model was conducted. Ghorbani et al. [2] established the coiler experimentalmodel, and the convective heat transfer of a coiler was studied. Based on the experimental data,the relationship between geometric size, operating conditions, and heat transfer performance wereanalyzed. Al-Hasan et al. [3] studied the coiled heat exchanger, which is embedded in a packedbed of spherical glass particles. The experiment was performed and a dimensionless correlationwas proposed. In [4], the effects of the coil pitch and the curvature ratio on the pressure drop andheat transfer behavior were analyzed experimentally with the Al2O3/water nanofluid laminar flow.The authors in [5] reported the experimental results of a conical coil heat exchanger with a 90◦ conicalcoil heat exchanger, and the thermal performance was studied thoroughly. Additionally, the empiricalcorrelations were proposed for predicting the Nusselt number. Other studies [6–11] have performedexperiments and the methods for enhanced heat transfer of coils are proposed.

Energies 2017, 10, 1982; doi:10.3390/en10121982 www.mdpi.com/journal/energies

Energies 2017, 10, 1982 2 of 13

The numerical studies on coil heat exchangers also widely exist in various areas of the literatureand they are proved to be accurate and show high performance. In [12], the authors establisheda model of vertical helically-coiled tubes in a cylindrical shell, the effects of the Reynolds number,coil-to-tube diameter ratios, non-dimensional coil pitches, and Rayleigh numbers on mixed convectionheat transfer were numerically studied. Nada et al. [13] performed studies on a helically-coiled heatexchanger by using the FLUENT 14.5 CFD package (ANSYS, Inc., Canonsburg, PA, USA), and thecharacteristics of heat transfer were discussed. Additionally, the numerical results are validated by acomparison with previous experimental data. Moraveji et al. [14] carried out the investigation of ahorizontal helically-coiled tube with CuO/oil-based nanofluid on the basis of the computationalfluid dynamics (CFD) method. The Nusselt number was estimated by four correlations in thepaper. Raju et al. [15] and Lele et al. [16] established the modelling of a helical coil heat exchangerwith COMSOL software, respectively, and studied the heat transfer characteristics of the exchanger.In [17–23], the numerical simulations on coil heat exchangers were conducted and the optimizations ofexchangers were explored.

Ice is the typical phase change material, which has many applications in the engineering field.The ice storage system has the advantages of large specific heat capacity and low cost. Yang et al. [24]studied thermal energy storage units, and the dynamic melting process of the phase change materialwas studied, investigated by means of experimental measurements and numerical simulations.The comprehensive solution of investigation on the heat exchange process of the thermal energystorage system using phase change material was provided. Carbonell et al. [25] established the modelof an ice storage tank with heat exchangers. The investigation on main variables, such as the massof ice and outlet temperature, were carried out, and the predictive capability of the model provedto be accurate. Zheng et al. [26] studied the charging and discharging process of an internal meltice-on-coil thermal storage system on the basis on experiment, and the comparison between simulationand experiment was carried out.

Most of the studies have focused on the coil heat exchanger, which rarely involves the coil heatexchanger with an ice storage system. In this work, the study of a coil heat exchanger with an icestorage system is performed. We carry out three aspects of research, including theoretical analysis,numerical simulation, and experiment, to study the coil heat exchanger with an ice storage system.Moreover, this study has reference value for the enhanced heat transfer of coil heat exchangers and theapplication of phase change material.

2. Theoretical Analysis

2.1. Model of Ice Storage System

Water is utilized as the phase change medium in the system, which could be used for the coolingof fluid in the coil structure. The system is equipped with a stirring blade to enhance convective heattransfer. Figure 1 shows the structure of the ice storage cooling water system. These systems aremainly composed of evaporating pipe, a drinking water pipe, an agitator, and a container. There isa cold preservation layer on the surface of the container, and the surface can be regarded as theadiabatic condition.

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The numerical studies on coil heat exchangers also widely exist in various areas of the literature and they are proved to be accurate and show high performance. In [12], the authors established a model of vertical helically-coiled tubes in a cylindrical shell, the effects of the Reynolds number, coil-to-tube diameter ratios, non-dimensional coil pitches, and Rayleigh numbers on mixed convection heat transfer were numerically studied. Nada et al. [13] performed studies on a helically-coiled heat exchanger by using the FLUENT 14.5 CFD package (ANSYS, Inc., Canonsburg, PA, USA), and the characteristics of heat transfer were discussed. Additionally, the numerical results are validated by a comparison with previous experimental data. Moraveji et al. [14] carried out the investigation of a horizontal helically-coiled tube with CuO/oil-based nanofluid on the basis of the computational fluid dynamics (CFD) method. The Nusselt number was estimated by four correlations in the paper. Raju et al. [15] and Lele et al. [16] established the modelling of a helical coil heat exchanger with COMSOL software, respectively, and studied the heat transfer characteristics of the exchanger. In [17–23], the numerical simulations on coil heat exchangers were conducted and the optimizations of exchangers were explored.

Ice is the typical phase change material, which has many applications in the engineering field. The ice storage system has the advantages of large specific heat capacity and low cost. Yang et al. [24] studied thermal energy storage units, and the dynamic melting process of the phase change material was studied, investigated by means of experimental measurements and numerical simulations. The comprehensive solution of investigation on the heat exchange process of the thermal energy storage system using phase change material was provided. Carbonell et al. [25] established the model of an ice storage tank with heat exchangers. The investigation on main variables, such as the mass of ice and outlet temperature, were carried out, and the predictive capability of the model proved to be accurate. Zheng et al. [26] studied the charging and discharging process of an internal melt ice-on-coil thermal storage system on the basis on experiment, and the comparison between simulation and experiment was carried out.

Most of the studies have focused on the coil heat exchanger, which rarely involves the coil heat exchanger with an ice storage system. In this work, the study of a coil heat exchanger with an ice storage system is performed. We carry out three aspects of research, including theoretical analysis, numerical simulation, and experiment, to study the coil heat exchanger with an ice storage system. Moreover, this study has reference value for the enhanced heat transfer of coil heat exchangers and the application of phase change material.

2. Theoretical Analysis

2.1. Model of Ice Storage System

Water is utilized as the phase change medium in the system, which could be used for the cooling of fluid in the coil structure. The system is equipped with a stirring blade to enhance convective heat transfer. Figure 1 shows the structure of the ice storage cooling water system. These systems are mainly composed of evaporating pipe, a drinking water pipe, an agitator, and a container. There is a cold preservation layer on the surface of the container, and the surface can be regarded as the adiabatic condition.

Figure 1. Schematic of the ice storage system: (a) graphic model of the device; and (b) simplified cross section.

Figure 1. Schematic of the ice storage system: (a) graphic model of the device; and (b) simplifiedcross section.

The container is filled with medium water. The evaporating pipe, drinking water pipe, and agitatorare immersed in the medium water. The evaporator pipe is externally connected to the compressor.The water in the container is frozen, and the ice is adhered to the surface of the evaporating pipewhen the compressor is working. The physical parameters of the water and ice are shown in Table 1.In another circulating system, drinking water flows in the water coil, releasing heat and reducing itstemperature. During the freezing process, the agitation of the blades will prevent the formation oftemperature stratification, so that the thickness of the ice layer outside the evaporator tube is uniform.

Table 1. Physical parameters of water and ice.

Physical Parameters Water Ice

Density (kg/m3) 999.9 913Specific heat capacity (J/kg·K) 4212 2100

Thermal conductivity (W/(m·K)) 0.54 2.22Viscosity (Pa·s) 0.0018 -

Melting heat (J/kg) 333,146 333,146Phase change point (K) 273.16 273.16

2.2. Theoretical Analysis

Figure 2 shows the simplified model of the evaporation coil and its simplified model of heattransfer with phase change. The refrigerant absorbs heat in the coil shown in Figure 2a. The materialof the evaporating coil pipe is copper, its external diameter is 8 mm, and there are gaps between thecoils, which is favorable for preventing the ice to be completely detached away from the evaporationtube in the melting process.

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The container is filled with medium water. The evaporating pipe, drinking water pipe, and agitator are immersed in the medium water. The evaporator pipe is externally connected to the compressor. The water in the container is frozen, and the ice is adhered to the surface of the evaporating pipe when the compressor is working. The physical parameters of the water and ice are shown in Table 1. In another circulating system, drinking water flows in the water coil, releasing heat and reducing its temperature. During the freezing process, the agitation of the blades will prevent the formation of temperature stratification, so that the thickness of the ice layer outside the evaporator tube is uniform.

Table 1. Physical parameters of water and ice.

Physical Parameters Water Ice Density (kg/m3) 999.9 913

Specific heat capacity (J/kg·K) 4212 2100 Thermal conductivity (W/(m·K)) 0.54 2.22

Viscosity (Pa·s) 0.0018 - Melting heat (J/kg) 333,146 333,146

Phase change point (K) 273.16 273.16

2.2. Theoretical Analysis

Figure 2 shows the simplified model of the evaporation coil and its simplified model of heat transfer with phase change. The refrigerant absorbs heat in the coil shown in Figure 2a. The material of the evaporating coil pipe is copper, its external diameter is 8 mm, and there are gaps between the coils, which is favorable for preventing the ice to be completely detached away from the evaporation tube in the melting process.

Figure 2. Evaporation coil and its simplified model of heat transfer with phase change: (a) 2D model of the evaporation coil; and (b) unsteady heat transfer in the ice storage process.

Since the evaporating tube is cylinder-shaped, its physical model can be regarded as the problem of unsteady heat transfer in cylindrical coordinates. Its simplified model is shown in Figure 2b. The evaporation tube can be considered as a cylinder structure and its diameter is 50 mm. The inner diameter evaporation tube is 6 mm and its wall thickness is 0.05 mm. Thus, the outside radius of the cylinder structure (R1) is 53.5 mm. The height of evaporation coil (h) is 150 mm. The freezing process start from the position of outside radius of cylinder structure. In this section, the variation of the ice layer thickness and temperature distributions in the ice storage system are solved based on the unsteady heat transfer equation [27]. Furthermore, the purpose of this paper is to develop the practical application of ice storage based on the analytical solution. The design of exchanger includes two parts: the evaporator coil as the cold source to absorb heat in the medium water, and the drinking water coil which is also submerged in the medium water as the heat source. The drinking water in the coil can be cooled down by medium water.

The differential equation of heat conduction in the solid phase region:

Figure 2. Evaporation coil and its simplified model of heat transfer with phase change: (a) 2D model ofthe evaporation coil; and (b) unsteady heat transfer in the ice storage process.

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Since the evaporating tube is cylinder-shaped, its physical model can be regarded as the problemof unsteady heat transfer in cylindrical coordinates. Its simplified model is shown in Figure 2b.The evaporation tube can be considered as a cylinder structure and its diameter is 50 mm. The innerdiameter evaporation tube is 6 mm and its wall thickness is 0.05 mm. Thus, the outside radius ofthe cylinder structure (R1) is 53.5 mm. The height of evaporation coil (h) is 150 mm. The freezingprocess start from the position of outside radius of cylinder structure. In this section, the variation ofthe ice layer thickness and temperature distributions in the ice storage system are solved based on theunsteady heat transfer equation [27]. Furthermore, the purpose of this paper is to develop the practicalapplication of ice storage based on the analytical solution. The design of exchanger includes two parts:the evaporator coil as the cold source to absorb heat in the medium water, and the drinking water coilwhich is also submerged in the medium water as the heat source. The drinking water in the coil can becooled down by medium water.

The differential equation of heat conduction in the solid phase region:

∂ts

∂τ= as

1r

∂

∂r

(r

∂ts

∂r

), R1 < r < r(τ), τ > 0 (1)

The differential equation of heat conduction in the liquid phase region:

∂tl∂τ

= al1r

∂

∂r

(r

∂tl∂r

), r(τ) < r < R2, τ > 0 (2)

The coupling condition of temperature and heat transfer on the two-phase interface:

ts = tl = tm = 273.16K, r = r(τ), τ > 0 (3)

λs∂ts

∂r− λl

∂tl∂r

= ρsL∂r∂τ

, r = r(τ), τ > 0 (4)

The temperature distribution in the solid and liquid phases are the following:

ts(r, τ) = A− BEi[−(r− R1)

2

4asτ], R1 < r < r(τ) (5)

tl(r, τ) = t0 − CEi[−(r− R1)

2

4alτ], r(τ) < r < R2 (6)

Ei(z) =∫ x

−∞

eu

udu (7)

where Ei(z) is the exponential integral function.The derivation of temperature distribution in the solid and liquid phases:

∂ts

∂r=

2Br− R1

exp[− (r− R1)2

4asτ], R1 < r < r(τ) (8)

∂tl∂r

=2C

r− R1exp[− (r− R1)

2

4alτ], r(τ) < r < R2 (9)

Heat absorbed from the energy-storage material:

ql = limr→R1

(2πrλs∂ts

∂r) = −211.43λsB exp(−0.0032/4asτ) (10)

B = −ql/[211.43λs exp(−0.0032/4asτ)] (11)

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The coupling condition of temperature on the two-phase interface can be described as follows:

A +ql

4πλsEi

[− (r− R1)

2

4asτ

]= t0 − CEi

[− (r− R1)

2

4alτ

]= tm, r = r(τ), τ > 0 (12)

This equation is valid for any moment with different τ; then:

(r− R1)2

4alτ= η2 (13)

where η is the undetermined constant. Thus, the outside ice radius is: r(τ) = R1 + 2η√

alτ.The values of A and C are as follows:

A = tm −ql

4πλsEi(−η2) (14)

C =t0 − tm

Ei(−η2as/al)(15)

The coupling condition of heat transfer on the two-phase interface can be described as follows:

ql4π

exp(−η2) +λl(t0 − tm)

Ei(−η2 asal)

exp(−η2 as

al) = η2asρsL (16)

The temperature of water t0 is 273.2 K.The power of the refrigerator is 66 W and ql is obtained:

ql =wh= 440 W/m (17)

where h is the height of the evaporation coil.

36.22 exp(−η2)− 0.0216Ei(−8.78η2)

exp(−8.78η2)− 350η2 = 0 (18)

Subsequently, we can obtain the value of η.The solution of the ice thickness variation is:

δ = r(τ)− Rl = 0.000724η × τ0.5 (19)

It can be observed from Equation (19) that the ice thickness variation is in direct proportion to the0.5 power of time.

3. Numerical Study

Numerical simulation is utilized to determine the agitator’s position and examine its influence onheat transfer efficiency. In our simulation, the temperature of the water in coil structure is 293.15 K,and the velocity of water in the coil structure is 0.84 m/s. The temperatures of the ice layer is 273.15 K,and the temperature of the medium water is 273.2 K. The initial thickness of the ice layer is 16 mm.The fluid is in a turbulent state and the viscosity is ignored. The heat conduction inside the wall of thedrinking water pipe is set as one-dimensional heat conduction, discarding the radiation heat transferin the system.

3.1. Numerical Method

FLUENT 16.0 CFD package (ANSYS, Inc., Canonsburg, PA, USA) is employed to perform thenumerical study. The shape of the mesh is tetrahedral. Mesh independence of the numerical model

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has been performed and the total number of computational meshes is four million. The form ofpressure-velocity coupling is SIMPLE. The turbulent kinetic energy form is second-order upwind.In detail, the solidification and melting model is used for the phase change of the coil heat exchangerwith an ice storage system. The conservation equations of mass, momentum, and energy equation areas follows [28,29]:

Mass continuity equation:∂ρ

∂t+∇ · (ρ→ν ) = 0 (20)

Momentum conservation equation:

∂

∂t(ρ→ν ) +∇ · (ρ→ν→ν ) = −∇P + ρg +

→f (21)

Energy conservation equation:

∂

∂t[ρe] +∇ · [(ρe + P)

→ν ] = ∇ · (λ∇T −∑

jhj→J j + (

→τ e f f ·

→ν )) (22)

where t is the time, ρ is the mass density, P represents the fluid pressure,→ν is the flow velocity, e is

the inside energy per unit mass,→f shows the volumetric force, λ is the thermal conductivity, hj is the

enthalpy of species j,→J j represents the diffusion flux of species j and, finally,

→τ e f f exhibits the stress

tensor. The rotary speed of the blade is high, the variation of the fluid velocity is frequent, and theRNG k-ε viscous model is employed to carry out the numerical simulation.

3.2. Analysis of Numerical Results

3.2.1. Effect of the Agitator Height on the Flow Field

Figure 3 shows the diagram of velocity distribution of the coil heat exchanger with differentagitator heights. The height of the agitator in the system is positioned at 40 mm (Figure 3a), 60 mm(Figure 3b), 80 mm (Figure 3c), and 100 mm (Figure 3d). It can be concluded from the figure that theexistence of the agitator has a significant impact on the flow field. The high rotation speed (2500 r/min)of the agitator makes the medium water in the container form a circulating flow. The medium waterflows downwards from the middle of the container to the gap between the coil pipe and the bottom ofthe container, and then flows upward through the outer gap between the ice layer and the container,finally flowing back to the middle of the system through the top. The flow field has few vortices withthe agitator height of 40 mm, and the vortex intensity increases with the increasing agitator height.For the practical application of an ice storage refrigeration system, the addition of stirring bladescan increase the flow rate of the medium fluid, so that the convective heat transfer coefficient of thestructure is enlarged, and the heat exchange efficiency of the system is enhanced.

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jh is the enthalpy of species j, jJ

represents the diffusion flux of species j and, finally, τ eff exhibits

the stress tensor. The rotary speed of the blade is high, the variation of the fluid velocity is frequent, and the RNG k-ε viscous model is employed to carry out the numerical simulation.

3.2. Analysis of Numerical Results

3.2.1. Effect of the Agitator Height on the Flow Field

Figure 3 shows the diagram of velocity distribution of the coil heat exchanger with different agitator heights. The height of the agitator in the system is positioned at 40 mm (Figure 3a), 60 mm (Figure 3b), 80 mm (Figure 3c), and 100 mm (Figure 3d). It can be concluded from the figure that the existence of the agitator has a significant impact on the flow field. The high rotation speed (2500 r/min) of the agitator makes the medium water in the container form a circulating flow. The medium water flows downwards from the middle of the container to the gap between the coil pipe and the bottom of the container, and then flows upward through the outer gap between the ice layer and the container, finally flowing back to the middle of the system through the top. The flow field has few vortices with the agitator height of 40 mm, and the vortex intensity increases with the increasing agitator height. For the practical application of an ice storage refrigeration system, the addition of stirring blades can increase the flow rate of the medium fluid, so that the convective heat transfer coefficient of the structure is enlarged, and the heat exchange efficiency of the system is enhanced.

Figure 3. Diagram of velocity distribution of the coil heat exchanger with different agitator heights. (a) h = 40 mm; (b) h = 60 mm; (c) h = 80 mm; (d) h = 100 mm.

3.2.2. Effect of Agitator Height on Fluid Turbulence Intensity

Figure 4 shows the effect of agitator height on fluid turbulence intensity. In this simulation, by adjusting the height of the agitator, the flow field in the system is analyzed to determine the influence of the blade position on the convective heat transfer coefficient. The average ice thickness was 3 mm, so we just set the ice as a solid part without phase change in our flow field simulation.

Figure 4. Distribution of fluid turbulence intensity in the system. (a) h = 40 mm; (b) h = 60 mm; (c) h = 80 mm; (d) h = 100 mm.

The cooling of drinking water is mainly caused by convective heat transfer, so the higher part of the medium water would be better cooled. At the same time, the melting of the ice provides refrigeration power, and the greater flow rate of the medium water would improve the ice melting.

Figure 3. Diagram of velocity distribution of the coil heat exchanger with different agitator heights.(a) h = 40 mm; (b) h = 60 mm; (c) h = 80 mm; (d) h = 100 mm.

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3.2.2. Effect of Agitator Height on Fluid Turbulence Intensity

Figure 4 shows the effect of agitator height on fluid turbulence intensity. In this simulation,by adjusting the height of the agitator, the flow field in the system is analyzed to determine theinfluence of the blade position on the convective heat transfer coefficient. The average ice thicknesswas 3 mm, so we just set the ice as a solid part without phase change in our flow field simulation.

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jh is the enthalpy of species j, jJ

represents the diffusion flux of species j and, finally, τ eff exhibits

the stress tensor. The rotary speed of the blade is high, the variation of the fluid velocity is frequent, and the RNG k-ε viscous model is employed to carry out the numerical simulation.

3.2. Analysis of Numerical Results

3.2.1. Effect of the Agitator Height on the Flow Field

Figure 3 shows the diagram of velocity distribution of the coil heat exchanger with different agitator heights. The height of the agitator in the system is positioned at 40 mm (Figure 3a), 60 mm (Figure 3b), 80 mm (Figure 3c), and 100 mm (Figure 3d). It can be concluded from the figure that the existence of the agitator has a significant impact on the flow field. The high rotation speed (2500 r/min) of the agitator makes the medium water in the container form a circulating flow. The medium water flows downwards from the middle of the container to the gap between the coil pipe and the bottom of the container, and then flows upward through the outer gap between the ice layer and the container, finally flowing back to the middle of the system through the top. The flow field has few vortices with the agitator height of 40 mm, and the vortex intensity increases with the increasing agitator height. For the practical application of an ice storage refrigeration system, the addition of stirring blades can increase the flow rate of the medium fluid, so that the convective heat transfer coefficient of the structure is enlarged, and the heat exchange efficiency of the system is enhanced.

Figure 3. Diagram of velocity distribution of the coil heat exchanger with different agitator heights. (a) h = 40 mm; (b) h = 60 mm; (c) h = 80 mm; (d) h = 100 mm.

3.2.2. Effect of Agitator Height on Fluid Turbulence Intensity

Figure 4 shows the effect of agitator height on fluid turbulence intensity. In this simulation, by adjusting the height of the agitator, the flow field in the system is analyzed to determine the influence of the blade position on the convective heat transfer coefficient. The average ice thickness was 3 mm, so we just set the ice as a solid part without phase change in our flow field simulation.

Figure 4. Distribution of fluid turbulence intensity in the system. (a) h = 40 mm; (b) h = 60 mm; (c) h = 80 mm; (d) h = 100 mm.

The cooling of drinking water is mainly caused by convective heat transfer, so the higher part of the medium water would be better cooled. At the same time, the melting of the ice provides refrigeration power, and the greater flow rate of the medium water would improve the ice melting.

Figure 4. Distribution of fluid turbulence intensity in the system. (a) h = 40 mm; (b) h = 60 mm;(c) h = 80 mm; (d) h = 100 mm.

The cooling of drinking water is mainly caused by convective heat transfer, so the higher partof the medium water would be better cooled. At the same time, the melting of the ice providesrefrigeration power, and the greater flow rate of the medium water would improve the ice melting.When the height of the blade is 80 mm, the turbulence intensity of the fluid near the wall of the heatexchanger is the largest, and the range is the widest. Based on the simulation results, the convectiveheat transfer coefficient is obtained, when the height of the agitator was 40, 60, 80, and 100 mm,the convective heat transfer coefficient of the drinking water pipe was 1728 W/m2·K, 2018 W/m2·K,2543 W/m2·K, and 2104 W/m2·K, respectively. As a result, the heat transfer coefficient of the drinkingwater pipe wall is the highest when the blade height is 80 mm.

3.2.3. Process of Ice Melting

Figure 5 shows the ice melting variation chart, and the color in the picture indicates the proportionof the water. ‘Blue’ means there is 100% solid water, and ‘red’ indicates 100% liquid water. Since thesimulation is mainly concerned with the melting of ice, the simulation results just shows the proportionof ice and water. As it is shown in the figure, due to the rapid flow and the large turbulence intensityof the medium water at the bottom of the container. The melting process begins from the lower part ofice layer, and the ice in the top part of coil structure finally melts. In the experimental study (Section 4),it can be observed from the temperature variation that the temperature at point 1 rises to 0 ◦C firstly,meaning that the melting process begins from the lower part of the layer. Thus, the numerical resultsagree well with the experimental results through qualitative analysis, and it follows that the numericalstudy is capable of simulating the melting process of the ice storage system. Combined with thevelocity distribution, due to the medium water close to the container wall cycling faster, the ice heremelts faster than the inside. It can be observed that while the system is working, the medium water isnot 100% pure liquid water, and the medium consists of a solid-liquid mixed fluid. All of the ice finallymelted at 174 s.

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When the height of the blade is 80 mm, the turbulence intensity of the fluid near the wall of the heat exchanger is the largest, and the range is the widest. Based on the simulation results, the convective heat transfer coefficient is obtained, when the height of the agitator was 40, 60, 80, and 100 mm, the convective heat transfer coefficient of the drinking water pipe was 1728 W/m2·K, 2018 W/m2·K, 2543 W/m2·K, and 2104 W/m2·K, respectively. As a result, the heat transfer coefficient of the drinking water pipe wall is the highest when the blade height is 80 mm.

3.2.3. Process of Ice Melting

Figure 5 shows the ice melting variation chart, and the color in the picture indicates the proportion of the water. ‘Blue’ means there is 100% solid water, and ‘red’ indicates 100% liquid water. Since the simulation is mainly concerned with the melting of ice, the simulation results just shows the proportion of ice and water. As it is shown in the figure, due to the rapid flow and the large turbulence intensity of the medium water at the bottom of the container. The melting process begins from the lower part of ice layer, and the ice in the top part of coil structure finally melts. In the experimental study (Section 4), it can be observed from the temperature variation that the temperature at point 1 rises to 0 °C firstly, meaning that the melting process begins from the lower part of the layer. Thus, the numerical results agree well with the experimental results through qualitative analysis, and it follows that the numerical study is capable of simulating the melting process of the ice storage system. Combined with the velocity distribution, due to the medium water close to the container wall cycling faster, the ice here melts faster than the inside. It can be observed that while the system is working, the medium water is not 100% pure liquid water, and the medium consists of a solid-liquid mixed fluid. All of the ice finally melted at 174 s.

Figure 5. Ice melting variation with time (the height of the agitator was 80 mm). (a) τ = 0 s; (b) τ = 19 s; (c) τ = 54 s; (d) τ = 106 s; (e) τ = 124 s; (f) τ = 174 s.

3.2.4. Outlet Temperature

The temperature variation curve of the outlet is shown in the Figure 6. As it is shown in the figure, the temperature of the outlet water has a transient fluctuation after the start-up of the system. It decreases to 2 °C quickly, then the temperature of the outlet water is steady for about four minutes. Taken together, the heat transfer effect of the coil heat exchanger with an ice-cold system has proved to be extremely powerful.

Figure 6. Temperature variation curve of the outlet water.

Figure 5. Ice melting variation with time (the height of the agitator was 80 mm). (a) τ = 0 s; (b) τ = 19 s;(c) τ = 54 s; (d) τ = 106 s; (e) τ = 124 s; (f) τ = 174 s.

3.2.4. Outlet Temperature

The temperature variation curve of the outlet is shown in the Figure 6. As it is shown in thefigure, the temperature of the outlet water has a transient fluctuation after the start-up of the system.It decreases to 2 ◦C quickly, then the temperature of the outlet water is steady for about four minutes.Taken together, the heat transfer effect of the coil heat exchanger with an ice-cold system has proved tobe extremely powerful.

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When the height of the blade is 80 mm, the turbulence intensity of the fluid near the wall of the heat exchanger is the largest, and the range is the widest. Based on the simulation results, the convective heat transfer coefficient is obtained, when the height of the agitator was 40, 60, 80, and 100 mm, the convective heat transfer coefficient of the drinking water pipe was 1728 W/m2·K, 2018 W/m2·K, 2543 W/m2·K, and 2104 W/m2·K, respectively. As a result, the heat transfer coefficient of the drinking water pipe wall is the highest when the blade height is 80 mm.

3.2.3. Process of Ice Melting

Figure 5 shows the ice melting variation chart, and the color in the picture indicates the proportion of the water. ‘Blue’ means there is 100% solid water, and ‘red’ indicates 100% liquid water. Since the simulation is mainly concerned with the melting of ice, the simulation results just shows the proportion of ice and water. As it is shown in the figure, due to the rapid flow and the large turbulence intensity of the medium water at the bottom of the container. The melting process begins from the lower part of ice layer, and the ice in the top part of coil structure finally melts. In the experimental study (Section 4), it can be observed from the temperature variation that the temperature at point 1 rises to 0 °C firstly, meaning that the melting process begins from the lower part of the layer. Thus, the numerical results agree well with the experimental results through qualitative analysis, and it follows that the numerical study is capable of simulating the melting process of the ice storage system. Combined with the velocity distribution, due to the medium water close to the container wall cycling faster, the ice here melts faster than the inside. It can be observed that while the system is working, the medium water is not 100% pure liquid water, and the medium consists of a solid-liquid mixed fluid. All of the ice finally melted at 174 s.

Figure 5. Ice melting variation with time (the height of the agitator was 80 mm). (a) τ = 0 s; (b) τ = 19 s; (c) τ = 54 s; (d) τ = 106 s; (e) τ = 124 s; (f) τ = 174 s.

3.2.4. Outlet Temperature

The temperature variation curve of the outlet is shown in the Figure 6. As it is shown in the figure, the temperature of the outlet water has a transient fluctuation after the start-up of the system. It decreases to 2 °C quickly, then the temperature of the outlet water is steady for about four minutes. Taken together, the heat transfer effect of the coil heat exchanger with an ice-cold system has proved to be extremely powerful.

Figure 6. Temperature variation curve of the outlet water. Figure 6. Temperature variation curve of the outlet water.

4. Experimental Study

On the basis of theoretical analysis and numerical simulation, it is necessary to carry out anexperiment to verify the correctness of the result. The ice storage experiment system uses the phasechange of the medium water to achieve the effect of cold storage, and the system is equipped withan agitator to enhance convective heat transfer. The height of agitator is 80 mm with a rotationspeed of 2500 r/min. The experimental device including self-made ice storage cycle device, T-typethermocouple and data acquisition instrument. Figure 7 shows the arrangement of the thermocouples.The measuring point of thermocouple from bottom to up is named of point 1 to point 8, respectively.Before the experiment, ice water mixture was used to calibrate the all of the T-type thermocouples,and the data acquisition instrument was used to correct the deviation.

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4. Experimental Study

On the basis of theoretical analysis and numerical simulation, it is necessary to carry out an experiment to verify the correctness of the result. The ice storage experiment system uses the phase change of the medium water to achieve the effect of cold storage, and the system is equipped with an agitator to enhance convective heat transfer. The height of agitator is 80 mm with a rotation speed of 2500 r/min. The experimental device including self-made ice storage cycle device, T-type thermocouple and data acquisition instrument. Figure 7 shows the arrangement of the thermocouples. The measuring point of thermocouple from bottom to up is named of point 1 to point 8, respectively. Before the experiment, ice water mixture was used to calibrate the all of the T-type thermocouples, and the data acquisition instrument was used to correct the deviation.

Figure 7. Arrangement of thermocouple: (a) physical model; and (b) experiment.

Figure 8 shows the temperature variation of evaporating tube wall during the operation period. The position of thermocouple is shown in Figure 7. The thermocouple sticks to evaporation tube. When the coil heat exchanger is in the process of ice storage, the temperature in the evaporating tube increases with increasing height. As it is shown in figure, the super-cooling degree of the medium water near the inlet of the evaporator coil (measuring point 1) is large and reaches about −7 °C. From the evaporator coil upward, the super-cooling degree of the medium water decreases in turn. The temperature of the medium water near the middle of the evaporating coil (point 6) cannot be reduced to the triple point. The large super-cooling degree of the medium water is due to the large amount of heat absorbed by the refrigerant at the inlet of the evaporator coil, so it is considered to let the refrigerant flow from top to bottom through the evaporator coil in the application of the ice storage refrigeration system. Subsequently, the compressor stops working at 1500 s, and the ice storage refrigeration system starts the process of natural deicing. Since the drinking water flows continuously and brings heat in, the temperature of the medium water at every measuring point increases rapidly, and the temperature of the ice near the upper part of the evaporator coil passes through the triple points of the water and begins to melt at first. However, the temperature of the ice at the bottom of the vessel is still below the triple point, and the temperature rising process is relatively slow. After this, the temperature of the lower part of the ice passes the triple point at 1760 s and begins to melt: at this time the temperature of the upper part of the medium water has reached the maximum temperature of 4 °C. The compressor starts working again at 1800 s, the temperature of the medium water decreases, and begins another round of the ice storage process.

Figure 7. Arrangement of thermocouple: (a) physical model; and (b) experiment.

Figure 8 shows the temperature variation of evaporating tube wall during the operation period.The position of thermocouple is shown in Figure 7. The thermocouple sticks to evaporation tube.When the coil heat exchanger is in the process of ice storage, the temperature in the evaporating tubeincreases with increasing height. As it is shown in figure, the super-cooling degree of the mediumwater near the inlet of the evaporator coil (measuring point 1) is large and reaches about −7 ◦C.From the evaporator coil upward, the super-cooling degree of the medium water decreases in turn.The temperature of the medium water near the middle of the evaporating coil (point 6) cannot bereduced to the triple point. The large super-cooling degree of the medium water is due to the largeamount of heat absorbed by the refrigerant at the inlet of the evaporator coil, so it is considered tolet the refrigerant flow from top to bottom through the evaporator coil in the application of the icestorage refrigeration system. Subsequently, the compressor stops working at 1500 s, and the ice storagerefrigeration system starts the process of natural deicing. Since the drinking water flows continuouslyand brings heat in, the temperature of the medium water at every measuring point increases rapidly,and the temperature of the ice near the upper part of the evaporator coil passes through the triplepoints of the water and begins to melt at first. However, the temperature of the ice at the bottom of thevessel is still below the triple point, and the temperature rising process is relatively slow. After this,the temperature of the lower part of the ice passes the triple point at 1760 s and begins to melt: at thistime the temperature of the upper part of the medium water has reached the maximum temperature of4 ◦C. The compressor starts working again at 1800 s, the temperature of the medium water decreases,and begins another round of the ice storage process.Energies 2017, 10, 1982 9 of 12

Figure 8. Temperature variation of the evaporating tube wall during the operation period.

Figure 9 shows the temperature variation of the evaporating tube wall during the forced deicing period. The position of the thermocouple is shown in Figure 7 and the distance between the thermocouple and evaporation tube is 9 mm. The icing condition of the coil heat exchanger can be obtained by the temperature of the thermocouples. When the thermocouples are covered with ice, they open the outlet of the drinking water. The system continues to release ice water and the temperature variation curves of the evaporating tube wall during the forced deicing period is shown in the figure. It can be seen from the figure that the temperature of the thermocouple in the bottom position (measuring point 1) increases to 0 °C firstly, and the temperature of the thermocouples in the upper position (measuring points 6, 7, and 8) increase to 0 °C lastly. Melting occurs at the lower part of the ice layer first, and the deicing in the bottom position of the coil heat exchanger is more rapid than in the upper position. This could be explained by the analysis of flow characteristics of the medium water in the exchanger. The figure of the velocity distribution (Figure 3) shows that the medium water flows downwards from the middle of the container to the gap between the coil pipe and the bottom of the container firstly, and then flows upward through the outer gap between the ice layer and the container, finally flowing back to the middle of the system through the top. The heat transfer is in progress with the flow of the medium water. It can be concluded that the temperature of the medium water in the bottom portion of the coil structure is relatively higher through the flow characteristics of the medium water.

Figure 9. Temperature variation of the evaporating tube wall during the deicing period.

Figure 8. Temperature variation of the evaporating tube wall during the operation period.

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Figure 9 shows the temperature variation of the evaporating tube wall during the forced deicingperiod. The position of the thermocouple is shown in Figure 7 and the distance between thethermocouple and evaporation tube is 9 mm. The icing condition of the coil heat exchanger canbe obtained by the temperature of the thermocouples. When the thermocouples are covered withice, they open the outlet of the drinking water. The system continues to release ice water and thetemperature variation curves of the evaporating tube wall during the forced deicing period is shownin the figure. It can be seen from the figure that the temperature of the thermocouple in the bottomposition (measuring point 1) increases to 0 ◦C firstly, and the temperature of the thermocouples in theupper position (measuring points 6, 7, and 8) increase to 0 ◦C lastly. Melting occurs at the lower part ofthe ice layer first, and the deicing in the bottom position of the coil heat exchanger is more rapid thanin the upper position. This could be explained by the analysis of flow characteristics of the mediumwater in the exchanger. The figure of the velocity distribution (Figure 3) shows that the medium waterflows downwards from the middle of the container to the gap between the coil pipe and the bottomof the container firstly, and then flows upward through the outer gap between the ice layer and thecontainer, finally flowing back to the middle of the system through the top. The heat transfer is inprogress with the flow of the medium water. It can be concluded that the temperature of the mediumwater in the bottom portion of the coil structure is relatively higher through the flow characteristics ofthe medium water.

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Figure 8. Temperature variation of the evaporating tube wall during the operation period.

Figure 9 shows the temperature variation of the evaporating tube wall during the forced deicing period. The position of the thermocouple is shown in Figure 7 and the distance between the thermocouple and evaporation tube is 9 mm. The icing condition of the coil heat exchanger can be obtained by the temperature of the thermocouples. When the thermocouples are covered with ice, they open the outlet of the drinking water. The system continues to release ice water and the temperature variation curves of the evaporating tube wall during the forced deicing period is shown in the figure. It can be seen from the figure that the temperature of the thermocouple in the bottom position (measuring point 1) increases to 0 °C firstly, and the temperature of the thermocouples in the upper position (measuring points 6, 7, and 8) increase to 0 °C lastly. Melting occurs at the lower part of the ice layer first, and the deicing in the bottom position of the coil heat exchanger is more rapid than in the upper position. This could be explained by the analysis of flow characteristics of the medium water in the exchanger. The figure of the velocity distribution (Figure 3) shows that the medium water flows downwards from the middle of the container to the gap between the coil pipe and the bottom of the container firstly, and then flows upward through the outer gap between the ice layer and the container, finally flowing back to the middle of the system through the top. The heat transfer is in progress with the flow of the medium water. It can be concluded that the temperature of the medium water in the bottom portion of the coil structure is relatively higher through the flow characteristics of the medium water.

Figure 9. Temperature variation of the evaporating tube wall during the deicing period.

Figure 9. Temperature variation of the evaporating tube wall during the deicing period.

5. Conclusions

In this work, the study of a coil heat exchanger with an ice storage system is conducted bytheoretical analysis, numerical analysis, and experimental analysis. The following conclusions canbe drawn:

1. The theoretical analysis of ice thickness variation in the ice storage process is performed by theunsteady heat transfer method in cylindrical coordinates, and the ice thickness variation is indirect proportion to the 0.5 power of time.

2. The numerical analysis of the coil heat exchanger is investigated on the basis of the computationalfluid dynamics method. The deicing in the bottom position of the coil heat exchanger is morerapid than the upper position and this agrees well with the experimental results. The turbulenceintensity of the fluid near the wall of the heat exchanger is the largest with an agitator height of80 mm, and its heat transfer coefficient of the drinking water pipe wall is the highest. Furthermore,the ice on the outer side of the evaporator tube close to the container wall melts faster than theinner side.

3. The experimental analysis is performed. In the process of ice storage, the temperature ofthe evaporating tube increases with increasing height in the process of ice storage and thesuper-cooling degree of the medium water at the bottom is larger. In the process of deicing,

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the temperature of the thermocouple in the bottom position reaches 0 ◦C firstly, and meltingoccurs at the lower part of the ice layer.

6. Patents

Refrigerated container with ice storage system. Patent for utility model: ZL 2017 2 0146839.5,authorized by State Intellectual Property Office of the P.R.C., 2017.

Nomenclature

ts Temperature of solid phasetl Temperature of liquid phaseas Thermal diffusivity of solid phaseal Thermal diffusivity of liquid phaser Radius of ice layerR1 Radius of coil structureλs Thermal conductivity of solid phaseλl Thermal conductivity of liquid phaseρ Densityτ TimeL Melting heatA, B, C, η Undetermined coefficientE(i) Exponential integral functionql Heat flux of hot linew Power of refrigeratorh Height of evaporation coilδ Ice thicknessP Fluid pressure→ν Velocity vectore Inside energy→f Volumetric force

hj Enthalpy of species j→J j Diffusion flux of species j→τ e f f Stress tensor

Acknowledgments: This work is supported by the National Natural Science Foundation of China (no. 51376164),Joint Fund Project (no. 6141A02033507) and the Key Research and Development Program of Shandong Province(no. 2017GHY15113).

Author Contributions: Yan Li conceived and designed the experiments; Zhe Yan performed the theoreticalanalysis and wrote the paper; Chao Yang and Han Yuan analyzed the data; Bin Guo performed the experiments;Jian Zhao and Ning Mei conducted numerical simulation.

Conflicts of Interest: The authors declare no conflict of interest.

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